A tower internals and a gas-liquid mass transfer method using the same

Abstract

This invention discloses a column internal and a gas-liquid mass transfer method using the column internal. The column internal can be applied in distillation or absorption processes and is disposed between adjacent trays. It includes at least: an upper tray channel, which is located at the first opening of the upper tray and has multiple openings; a gap is left between the bottom of the upper tray channel and the upper tray for drawing liquid phase from the upper tray into the upper tray channel during the gas phase flow stage, and guiding the liquid phase of the upper tray into the space between the upper and lower trays during the initial stage of liquid phase flow; a gas phase spray hole is provided on the upper part of the upper tray channel wall for spraying out the drawn liquid phase carried by the gas phase and breaking large bubbles into small bubbles, and performing gas-liquid mass transfer at the upper tray; a movable component, which includes multiple upper circular surfaces and a single lower circular surface fixedly connected; when the movable component moves to the top under the support of the gas phase, it is in the gas phase flow stage; when the movable component moves downward under the gravity of the liquid phase, it is in the liquid phase flow stage; when the movable component moves to the bottom, the first opening and the second opening are closed.

Description

Technical Field

[0001] This invention relates to the field of petrochemical separation technology, and in particular to a tower internal and a gas-liquid mass transfer method using the tower internal. Background Technology

[0002] Distillation is a separation process that separates components in a mixture based on their different volatility. As the most widely used and technologically mature chemical separation technology, distillation uses heat as the sole separating agent, requiring a large amount of high-temperature heat, resulting in high energy consumption and extremely low thermodynamic efficiency. Statistics show that the petroleum and chemical industry currently accounts for approximately 9% to 10% of my country's total energy consumption, with distillation units accounting for about one-third of this. Especially for large-scale organic chemical processes in the petrochemical industry, distillation energy consumption can reach or exceed 50% of the total process energy consumption. Low-carbon development in the separation field and energy conservation and consumption reduction in distillation processes will make a significant contribution to carbon emission reduction in the petroleum and chemical industry.

[0003] In existing technologies, during distillation and absorption processes, the gas phase flows axially from the lower tray to the upper tray within the column, while the liquid phase flows radially from the upper tray via the downcomer, through the receiving pan, and then downcomer to the lower tray. The difference between the two separation processes is that in distillation, the gas phase is generated by heating the bottom liquid phase with a heat source provided by the column body, while in absorption, the gas phase is generally a gaseous feed. During this gas-liquid contact process, due to the cross-flow distribution of the gas and liquid phases and the limitation of the tray liquid holdup, the contact time between the gas and liquid phases is short, resulting in insufficient mass transfer. Furthermore, to ensure that the liquid phase on the tray can flow from the receiving pan to the next downcomer, the bottom clearance height of the downcomer is generally less than the weir height, ensuring that the liquid on the tray can flow smoothly into the downcomer while preventing gas from entering the downcomer. This structure creates a radial gradient in the liquid layer, resulting in uneven liquid layer thickness on the trays. This causes the rising gas phase on the lower trays to tend to flow from the areas with thinner liquid layers. The uneven gas-liquid contact reduces tray efficiency and, consequently, increases energy consumption in the separation process.

[0004] Chinese patent application CN114146437A discloses a distillation column tray, a plate distillation column, and their applications, relating to the field of distillation equipment. The distillation column tray includes a porous tray, a downcomer, and downcomer packing. The axial direction of the downcomer intersects the surface of the porous tray, and the downcomer packing fills the inside of the downcomer. The pore size of the porous tray is 0.2–100 μm. When the gas phase flows through the porous tray, micron-sized bubbles are generated. The reduced bubble size increases the total surface area of ​​the bubbles, increasing the mass transfer interface area between the gas and liquid phases, prolonging the residence time of the gas phase, reducing the amount of liquid splashing after bubble breakage, and minimizing mist entrainment. This significantly improves the mass transfer effect and enables gas-liquid separation at higher foam layer heights, increasing the axial mass transfer space of the distillation column. The downcomer packing in this design allows for gas-liquid contact mass transfer, thereby achieving gas-liquid mass transfer across the entire column cross-section and significantly improving mass transfer efficiency.

[0005] Although this type of scheme uses the generation of micron-sized bubbles and the filling of packing material in the downcomer to improve the gas-liquid mass transfer effect, its technical concept is still a traditional existing technology and cannot avoid the problem that "the liquid layer on the tray is uneven, causing the rising gas phase on the lower tray to tend to flow from the position where the liquid layer is thinner".

[0006] Therefore, there is an urgent need for a column internal and a gas-liquid mass transfer method using such an internal. This method can not only enhance the gas-liquid contact process, reduce the radial non-uniformity of the liquid layer distribution on the tray, improve tray efficiency, and reduce the energy consumption of the gas-liquid separation process, but also solve the problem of high equipment investment and high operating costs caused by low tray efficiency.

[0007] The information disclosed in this background section is intended only to enhance the understanding of the overall background of the invention and should not be construed as an admission or in any way implying that the information constitutes prior art known to those skilled in the art. Summary of the Invention

[0008] The purpose of this invention is to provide a column internal and a gas-liquid mass transfer method using the column internal. Through the structural design of the column internal, the independent phase flow of the gas and liquid phases in the column can be controlled, and the gas and liquid phases can be made to move in a jet state on the tray. Large bubbles can be broken into small bubbles, thereby enhancing the gas-liquid contact process, reducing the radial non-uniformity of the liquid layer distribution on the tray, improving the tray efficiency, and reducing the operating energy consumption of the gas-liquid separation process.

[0009] To achieve the above objectives, according to a first aspect of the present invention, a column internal is provided, applicable to distillation or absorption processes, disposed between adjacent trays, and comprising at least: an upper tray channel, which is disposed at a first opening of the upper tray and has multiple openings; a gap is left between the bottom of the upper tray channel and the upper tray for drawing liquid phase from the upper tray into the upper tray channel during the gas phase flow stage, and guiding the liquid phase from the upper tray into the space between the upper and lower trays during the initial stage of liquid phase flow; and gas phase spray holes are provided on the upper part of the upper tray channel wall for spraying out the drawn liquid phase carried by the gas phase and breaking large bubbles into smaller ones. Bubbles are generated and gas-liquid mass transfer occurs at the upper tray. A movable component includes multiple upper circular surfaces and a single lower circular surface fixedly connected. The number of upper circular surfaces is the same as the number of channels in the upper tray and they can move up and down along the corresponding channels. The upper circular surfaces are adapted to the first opening diameter of the upper tray, and the lower circular surface is adapted to the second opening diameter of the lower tray. When the movable component moves to the top under the lifting action of the gas phase, it is in the gas phase flow stage. When the movable component moves downward under the gravity action of the liquid phase, it is in the liquid phase flow stage. When the movable component moves to the bottom, the upper circular surface closes the first opening, and the lower circular surface closes the second opening.

[0010] Furthermore, in the above technical solution, multiple first openings can be arranged symmetrically on the upper tray, and correspondingly, a single second opening is preferably arranged at the projection position of the center of symmetry on the lower tray.

[0011] Furthermore, in the above technical solution, the number of upper circular surfaces is preferably 2 to 4, and the area of ​​the lower circular surface is preferably not less than the area of ​​a single upper circular surface.

[0012] Furthermore, in the above technical solution, a connector is provided between the upper circular surface and the lower circular surface. The connector can be a frame structure, and the supporting part of the corresponding circular surface is located at the center of the circle; the movable part as a whole can be shaped like a wine glass.

[0013] Furthermore, in the above technical solution, a first flange is provided at the top of the upper tray channel, which can be used to limit the upward movement of the upper circular surface; a second flange is provided at the bottom of the upper tray channel and at the first opening, which can be used to limit the downward movement of the upper circular surface and close the first opening, and the second flange forms a stepped structure with the surface of the upper tray.

[0014] Furthermore, in the above technical solution, a third flange is provided at the second opening, which can be used to limit the downward movement of the lower circular surface and close the second opening. The third flange forms a stepped structure with the surface of the lower tray.

[0015] Furthermore, in the above technical solution, the internal components of the tower may also include: a control subunit, which is used to control the gas supply to the tower tray during the gas phase flow stage and stop the gas supply to the tower tray during the liquid phase flow stage, so that the gas phase and liquid phase of the tower tray can operate independently.

[0016] Furthermore, in the above technical solution, the upper tray (including the internal space of the upper tray channel) forms a gas-liquid contact space; the lower tray forms a liquid holding space.

[0017] Furthermore, in the above technical solution, a catalyst can be placed on the upper tray to enable simultaneous catalytic reaction and separation during gas-liquid contact.

[0018] Furthermore, in the above technical solution, the upper tower tray channel can be fixed to the upper tower tray by fasteners.

[0019] Furthermore, in the above technical solution, several drain holes can be provided in the middle of the first opening of the upper tray. The diameter of the drain holes can be 2 to 10 mm to ensure that the liquid phase in the upper tray can be completely transferred to the lower tray during the liquid phase flow stage.

[0020] Furthermore, in the above technical solution, the gas phase nozzle can be a multi-layered opening with an opening diameter of 5–20 mm.

[0021] Furthermore, in the above technical solution, multiple tower internals can be set between the upper and lower tower trays and arranged at uniform intervals; the upper and lower tower trays constitute a set of tower trays, and multiple sets of tower trays can be set inside the tower.

[0022] To achieve the above objectives, according to a second aspect of the present invention, the present invention provides a gas-liquid mass transfer method, employing any of the aforementioned column internals, comprising at least the following steps: A. Gas phase flow stage: controlling the gas flow through the trays, the gas phase lifts the lower circular surface of the movable component, causing the movable component to move upward as a whole until the upper circular surface moves to the first flange; during this process, the gas phase moves from bottom to top and enters the space between the upper and lower trays through the second opening of the lower tray, thereby lifting the upper circular surface while drawing in and carrying the liquid phase from the upper tray into the upper tray channel, and ejecting it from the gas phase nozzle, thus performing gas-liquid mass and heat transfer while breaking up the bubbles; B. Liquid phase flow stage: Control the tray to stop venting. The moving part moves downward as a whole under the gravity of the liquid phase until the upper circular surface moves to the second flange and the lower circular surface moves to the third flange. During this process, the liquid phase flows from the upper tray into the space between the upper and lower trays through the gap at the bottom of the upper tray channel, forming a liquid holding cavity on the lower tray. C. Next gas phase flow stage: Control the tray to vent again. The gas phase lifts the lower circular surface of the moving part, causing the moving part to move upward as a whole. In the initial stage of upward movement, the second opening of the lower tray acts as a drain hole to release the liquid phase in the liquid holding cavity to the next set of trays, and step A is repeated.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] 1) This invention uses multiple centrally symmetrical upper tray channels and movable components that can move freely up and down in the channels. The upper circular surface of the movable component can be controlled to move up and down in the corresponding upper tray channels by utilizing the lifting force of the rising gas phase and the gravity of the liquid phase. At the same time, the lower circular surface can selectively open or close the openings on the lower tray, so that the tray can achieve independent operation of the gas and liquid phases (independent phase flow). The gas phase rises from the upper tray channel (i.e., the first opening of the upper tray) to the upper tray. The main mass and heat transfer of gas and liquid occurs in the upper tray. That is, when the gas phase is running, the liquid phase in the upper tray can be in a relatively static state. There is no radial flow as in the prior art. When the gas phase runs to the upper tray and comes into contact with the liquid phase, it can effectively enhance the gas-liquid contact and reduce the back mixing problem that exists when the gas and liquid phases flow simultaneously, compared with the prior art.

[0025] 2) In the gas phase flow stage of this invention, due to the gap at the bottom of the channel and the presence of gas phase nozzles at the top of the channel, the liquid phase can form a small circulation between the upper tray and the upper tray channel. Moreover, the gas phase is sprayed from the upper tray channel into the liquid phase in the upper tray in a jet state, and large bubbles can be broken into small bubbles, thereby further promoting gas-liquid contact mass transfer. Since the liquid phase achieves small circulation in a local area, the thickness of the liquid phase in each region of the upper tray can remain basically unchanged. Therefore, the problem of "radial thickness unevenness" in the prior art does not exist.

[0026] 3) In this invention, when the liquid phase in the upper tray begins to flow to the lower tray, the gas flow is stopped. At this time, the gas phase does not flow and cannot enter the space between the upper and lower trays. This ensures both the contact mass transfer between the gas phase and the relatively stationary liquid phase in the upper tray, and the flow of the liquid phase to the lower tray after the gas-liquid mass transfer, so that it can be used by the next set of trays.

[0027] 4) This invention adopts the "intermittent gas supply" method, which controls the gas supply to the tray during the gas phase flow stage and stops the gas supply to the tray during the liquid phase flow stage, so that the gas phase and liquid phase of the tray can operate independently; the upper tray (including the space in the upper tray channel) can form a gas-liquid contact space; during the liquid phase flow stage, the lower tray forms a liquid holding space, making more rational use of space and making the overall design of the tray more compact;

[0028] 5) A catalyst can be placed on the upper tray of the present invention to enable catalytic reaction and separation to occur simultaneously during gas-liquid contact, which is especially beneficial for reactions under equilibrium control, thereby improving reaction conversion rate and product purity.

[0029] 6) Multiple tower internals of the present invention can be arranged between the upper and lower trays, and are evenly spaced; the upper and lower trays of the present invention constitute a set of trays, and multiple sets of trays can be arranged inside the tower. This arrangement effectively increases the throughput.

[0030] 7) The “liquid discharge” process of the present invention involves a short period of simultaneous gas and liquid movement and countercurrent contact, which can perform gas-liquid mass and heat transfer in the traditional sense. However, the present invention mainly performs gas-liquid mass and heat transfer between the flowing gas phase and the relatively stationary liquid phase in the upper tray. This is significantly different from the traditional gas-liquid mass transfer method. This short “liquid discharge” process will not adversely affect the core technical effect of the present invention, and can also achieve the gas-liquid mass and heat transfer effect of the prior art during the liquid discharge process.

[0031] The above description is merely an overview of the technical solution of the present invention. In order to better understand the technical means of the present invention and to implement it according to the contents of the specification, and to make the above and other objects, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with reference to the accompanying drawings. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of the internal structure of the tower of the present invention.

[0033] Figure 2 This is a schematic diagram of the moving parts in the tower internals of the present invention.

[0034] Figure 3 is a schematic diagram of the independent operation of the gas and liquid phases when the movable part of the present invention moves to different positions (wherein) Figure 3-A This is a schematic diagram of the gas phase flow stage; Figure 3-B This is a schematic diagram of the liquid phase flow stage during the downward movement of the moving part; Figure 3-C This is a schematic diagram showing the moving part moving to the bottom and the liquid phase flow stage ending. Figure 3-D This is a schematic diagram of the initial state of the next gas phase flow stage (solid arrows represent the gas phase, and dashed arrows represent the liquid phase).

[0035] Explanation of key figure labels:

[0036] 101-Upper tray, 1011-First opening, 102-Lower tray, 1021-Second opening;

[0037] 1-Inner components of the tower, 11-Upper tray channel, 111-Gas phase nozzle, 112-Bottom gap, 113-First flange, 114-Second flange, 115-Fixed component, 12-Moving component, 121-Upper circular surface, 122-Lower circular surface, 123-Upper circular surface support component, 124-Intermediate frame, 125-Lower circular surface fixing component, 126-Third flange. Detailed Implementation

[0038] The specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings, but it should be understood that the scope of protection of the present invention is not limited to the specific embodiments.

[0039] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0040] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “upper,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0041] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0042] like Figure 1 As shown in Figure 3, the present invention provides a column internal 1, which can be applied in similar separation fields such as distillation processes, absorption processes, or special distillation processes. This column internal 1 is installed on adjacent trays (i.e.,...) Figure 1 The tower internals 1 of the present invention can be arranged between the upper and lower trays (101 and 102). Multiple trays can be evenly spaced between the upper and lower trays. The upper and lower trays form a group of trays, and multiple groups of such trays can be arranged within the tower (i.e., each group of trays includes similar components). Figure 1 Upper tray 101 and lower tray 102).

[0043] like Figure 1 As shown in Figure 3, the tower internal component 1 of the present invention includes at least an upper tray channel 11 and a movable component 12. The upper tray channel 11 can be fixed to the upper tray 101 by a fixing component 115. The upper tray channel 11 is disposed at the first opening 1011 of the upper tray 101 and has multiple ( Figure 1 The embodiment shown in the text depicts two first openings, but there are actually three, and they are consistent with... Figure 2(The three upper circular surfaces of the moving part 12 correspond to each other). Preferably, but not limitingly, the plurality of first openings 1011 can be arranged centrally symmetrically on the upper tray 101. A gap 112 is left between the bottom of the upper tray channel 11 and the upper tray 101 for drawing liquid phase from the upper tray 101 into the upper tray channel 11 during the gas phase flow stage, and guiding the liquid phase of the upper tray 101 into the space between the upper and lower trays in the initial stage of liquid phase flow. A gas phase spray hole 111 is provided on the upper wall of the upper tray channel 11 for spraying out the drawn liquid phase carried by the gas phase and breaking large bubbles into small bubbles, and performing gas-liquid mass transfer at the upper tray 101. The gas phase spray hole 111 can be a multi-layer opening, preferably 2 to 6 layers, and the opening diameter can be 5 to 20 mm, preferably 8 to 12 mm.

[0044] Further as Figure 1 As shown in Figure 3, the movable component 12 includes a plurality of upper circular surfaces 121 and a single lower circular surface 122 that are fixedly connected. Figure 2 The diagram illustrates three upper circular surfaces 121. The number of upper circular surfaces 121 is the same as the number of channels 11 on the upper tray and they can move up and down along the corresponding channels. The diameter of the upper circular surfaces 121 is matched with the diameter of the first opening 1011 of the upper tray 101, and the diameter of the lower circular surfaces 122 is matched with the diameter of the second opening 1021 of the lower tray 102. A single second opening 1021 can be arranged at the projection position of the symmetry center of the multiple upper circular surfaces 121 onto the lower tray 102 (see reference). Figure 2 The number of upper circular surfaces 121 can be 2 to 4, and the area of ​​the lower circular surfaces 122 is not less than the area of ​​a single upper circular surface 121. When the movable part 12 moves to the top under the action of gas phase lifting, it is the gas phase flow stage of the present invention (see reference). Figure 3-A (The solid arrow in the figure indicates the direction of gas phase flow). When the movable part 12 moves downward under the action of gravity of the liquid phase (at which time the gas supply stops), it is the liquid phase flow stage of the present invention (see reference). Figure 3-B and Figure 3-C (The dashed arrow in the diagram indicates the direction of liquid flow). When the movable part 12 moves to the bottom, the upper circular surface 121 closes the first opening 1011, and the lower circular surface 122 closes the second opening 1021. With this arrangement, the gas and liquid phases can be separated and flowed separately as needed at different stages.

[0045] This invention employs the aforementioned technical solution. Through multiple centrally symmetrically arranged upper tray channels and freely movable components within these channels, the upper circular surface of the movable components can be controlled to move up and down within the corresponding upper tray channels using the lifting force of the rising gas phase and the gravity of the liquid phase. Simultaneously, the lower circular surface can selectively open or close the openings on the lower tray, enabling the tray to achieve independent operation of the gas and liquid phases (independent phase flow). This allows the gas phase to rise from the upper tray channel (i.e., the first opening of the upper tray) to the upper tray. The main mass and heat transfer of the gas and liquid occurs in the upper tray. In other words, when the gas phase is running, the liquid phase in the upper tray can be in a relatively static state, eliminating the radial flow present in existing technologies (i.e., the radial thickness unevenness of the liquid phase caused by the use of downcomers). When the gas phase reaches the upper tray and contacts the liquid phase, this effectively enhances gas-liquid contact compared to existing technologies, reducing the backmixing problem that occurs when the gas and liquid phases flow simultaneously. It should be noted that during this process, due to the gap at the bottom of the channel and the presence of gas phase nozzles at the top of the channel, the liquid phase can form a small circulation between the upper tray and the upper tray channel, further promoting gas-liquid contact mass transfer. However, the thickness of the liquid phase in each region of the upper tray remains basically unchanged, thus avoiding the "radial thickness unevenness" problem mentioned in the prior art. More importantly, because the gas phase operates independently and the liquid phase in the upper tray is in a basically static state during the gas phase operation (only the aforementioned small circulation exists), the radial uniformity of the liquid layer in the upper tray can be significantly improved, thereby effectively improving the gas-liquid mass transfer efficiency, reducing the energy consumption of the separation process, and reducing equipment investment. When the liquid phase in the upper tray begins to flow to the lower tray (i.e., through the gap at the bottom of the upper tray channel), the gas flow is stopped. At this time, the gas phase does not flow and cannot enter the space between the upper and lower trays. This ensures both contact mass transfer between the gas phase and the relatively static liquid phase in the upper tray, and also ensures the flow of the liquid phase to the lower tray after gas-liquid mass transfer for use by the next set of trays.

[0046] Further as Figure 1 As shown, the upper tray channel 11 has a first flange 113 at the top, which can be used to limit the upward movement of the upper circular surface 121; the upper tray channel 11 has a second flange 114 at the bottom and the first opening 1011, which can be used to limit the downward movement of the upper circular surface 121 and close the first opening 1011. The second flange 114 and the surface of the upper tray 101 form a stepped structure (that is, the second flange 114 is recessed relative to the surface of the upper tray 101). The lower tray 102 has a third flange 126 at the second opening 1021, which can be used to limit the downward movement of the lower circular surface 122 and close the second opening. The third flange 126 and the surface of the lower tray 102 also form a stepped structure (that is, the third flange 126 is recessed relative to the surface of the lower tray 102, and this allows the lower circular surface 122 of the moving part to begin the liquid discharge process as soon as it leaves the third flange 126). Figure 3-D ).

[0047] Further as Figure 1 , 2 As shown, a connector is provided between the upper circular surface 121 and the lower circular surface 122. This connector can be an integral frame structure, with the supporting part of the corresponding circular surface located at the center. Specifically, the frame structure of the connector includes an upper circular surface support 123, a middle frame 124, and a lower circular surface fixing part 125. The upper circular surface support 123 is located at the center of the upper circular surface, the lower circular surface fixing part 125 is located at the center of the lower circular surface, and the middle frame 124 serves to connect the upper circular surface support 123 and the lower circular surface fixing part 125. The movable part 12 can be shaped like a wine glass.

[0048] Furthermore, this invention employs an "intermittent gas flow" method, which can be controlled by a control subunit (not shown in the figure) of the tower internals 1. The control subunit can be used to control the gas flow to the tray during the gas phase flow stage and to stop the gas flow to the tray during the liquid phase flow stage, allowing the gas and liquid phases of the tray to operate independently. During the gas phase flow stage, the upper tray 101 forms a gas-liquid contact space (gas-liquid contact also actually occurs within the upper tray channel, see reference...). Figure 3-A During the liquid phase flow stage, a liquid-holding space is formed in the lower tray 102 (reference). Figure 3-B and 3-C Furthermore, a catalyst can be placed on the upper tray 101 of the present invention to enable simultaneous catalytic reaction and separation during gas-liquid contact, which is particularly beneficial for equilibrium-controlled reactions, thereby improving reaction conversion rate and product purity. Multiple internal components 1 of the present invention can be arranged between the upper and lower trays at uniform intervals, effectively increasing throughput.

[0049] The present invention also provides a gas-liquid mass transfer method, which uses the aforementioned column internals 1 and includes at least the following steps:

[0050] Step S101, combined Figure 1 and Figure 3-AAs shown, this step is the gas phase flow stage: the control tray is ventilated, and the gas phase lifts the lower circular surface 122 of the movable component 12, causing the entire movable component to move upward until the upper circular surface 121 moves to the first flange 113; during this process, the gas phase moves from bottom to top and enters the space between the upper and lower trays through the second opening 1021 of the lower tray 102, thereby lifting the upper circular surface 121 while drawing in and carrying the liquid phase from the upper tray 101 into the upper tray channel 11, and spraying it out from the gas phase nozzle 111. While breaking up bubbles, gas-liquid mass and heat transfer also occur. In this step, due to the suction and carrying effect, the gas and liquid also mix and come into contact in the upper tray channel 11, forming a small liquid phase circulation between the upper tray 101 and the upper tray channel 11. Although this small circulation generates liquid phase flow, this flow is significantly different from the radial flow of liquid phase on the tray in the prior art. The present invention will not cause uneven thickness of the liquid phase on the tray due to radial flow, and this small circulation can also promote gas-liquid contact mass transfer.

[0051] Step S102, combined Figure 1 and Figure 3-B , Figure 3-C As shown, this step is the liquid phase flow stage: the control tray stops aeration, and the moving part 12 moves downward as a whole under the gravity of the liquid phase until the upper circular surface 121 moves to the second flange 114 and the lower circular surface 122 moves to the third flange 126; during this process, the liquid phase flows from the upper tray 101 into the space between the upper and lower trays through the gap 112 at the bottom of the upper tray channel 11, and forms a liquid holding cavity on the lower tray 102. Figure 3-B This is a schematic diagram of the moving part 12 moving downwards. At this time, the first opening 1011 of the upper tray 101 is still not closed, and the liquid phase of the upper tray 101 can flow into the space between the upper and lower trays through the gap 112 and the first opening 1011. Figure 3-C This is a schematic diagram of the movable part 12 moving down to the bottom. At this time, the second opening 1021 of the lower tray is closed by the lower circular surface 122 of the movable part, and the first opening 1011 of the upper tray is closed by the upper circular surface 121 of the movable part, forming a liquid holding cavity on the lower tray 102.

[0052] Step S103, combined Figure 1 and Figure 3-D As shown, in the next gas phase flow stage of this step: the tray venting is re-controlled, and the gas phase lifts the lower circular surface 122 of the movable component 12, causing the entire movable component to move upward; in the initial stage of upward movement, the second opening 1021 of the lower tray 102 serves as a drain hole (this is a brief draining process, that is, just as the lower circular surface 122 of the movable component leaves the third flange 126, the liquid phase can flow into the next set of trays from the gap, see reference). Figure 3-DThe liquid phase in the holding chamber can be released to the next set of trays, and step S101 can be repeated. It should be noted that at this time, the gas and liquid are moving simultaneously and in countercurrent contact, which can perform gas-liquid mass and heat transfer in the traditional sense. However, the main gas-liquid mass and heat transfer pursued by this invention occurs on the upper tray 101, that is, the gas-liquid mass and heat transfer between the flowing gas phase and the relatively stationary liquid phase mainly occurs on the upper tray. This is significantly different from the traditional gas-liquid mass transfer method. This brief "liquid discharge" process in this step will not adversely affect the core technical effect of this invention, and the gas-liquid mass and heat transfer effect of the prior art can be achieved during the liquid discharge process.

[0053] The foregoing description of specific exemplary embodiments of the present invention is for illustrative and explanatory purposes. These descriptions are not intended to limit the invention to the precise forms disclosed, and it will be apparent that many changes and variations can be made in accordance with the foregoing teachings. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application, thereby enabling those skilled in the art to implement and utilize various different exemplary embodiments of the invention, as well as various different choices and variations. Any simple modifications, equivalent changes, and alterations made to the foregoing exemplary embodiments should fall within the scope of protection of the present invention.

Claims

1. A column internal, characterized by, Used in distillation or absorption processes, positioned between adjacent trays, including: The upper tray channel is located at the first opening of the upper tray and has multiple openings. A gap is left between the bottom of the upper tray channel and the upper tray to draw liquid phase from the upper tray into the upper tray channel during the gas phase flow stage, and to guide the liquid phase from the upper tray into the space between the upper and lower trays in the initial stage of liquid phase flow. The upper wall of the upper tray channel is provided with gas phase spray holes to spray out the drawn liquid phase carried by the gas phase and break large bubbles into small bubbles, and to carry out gas-liquid mass transfer at the upper tray. The movable component includes multiple upper circular surfaces and a single lower circular surface that are fixedly connected. The number of upper circular surfaces is the same as the number of channels on the upper tray and they can move up and down along the corresponding channels. The upper circular surfaces are adapted to the first opening diameter of the upper tray, and the lower circular surface is adapted to the second opening diameter of the lower tray. When the movable component moves to the top under the action of gas phase lifting, it is in the gas phase flow stage. When the movable component moves downward under the action of liquid phase gravity, it is in the liquid phase flow stage. When the movable component moves to the bottom, the upper circular surface closes the first opening and the lower circular surface closes the second opening.

2. The tray insert of claim 1, wherein Multiple first openings are arranged symmetrically on the upper tray, and correspondingly, a single second opening is arranged at the projection position of the center on the lower tray.

3. The tray insert of claim 2, wherein, The number of upper circular surfaces is 2 to 4, and the area of ​​the lower circular surfaces is not less than the area of ​​a single upper circular surface.

4. The tray insert of claim 3, wherein, A connector is provided between the upper and lower circular surfaces. The connector is a frame structure, and the supporting part of the corresponding circular surface is located at the center. The movable part is shaped like a wine glass.

5. The tray insert of claim 1, wherein, The upper tray channel is provided with a first flange at the top for limiting the upward movement of the upper circular surface; the upper tray channel is provided with a second flange at the bottom and the first opening for limiting the downward movement of the upper circular surface and closing the first opening, and the second flange forms a stepped structure with the surface of the upper tray.

6. The tray insert of claim 1, wherein A third flange is provided at the second opening to limit the downward movement of the lower circular surface and close the second opening. The third flange forms a stepped structure with the surface of the lower tray.

7. The tray insert of claim 1, wherein The tower internals also include: A control subunit is used to control the gas flow to the tray during the gas phase flow stage and to stop the gas flow to the tray during the liquid phase flow stage, so that the gas and liquid phases of the tray operate independently.

8. The tray insert of claim 1, wherein, The upper tray forms a gas-liquid contact space; the lower tray forms a liquid holding space.

9. The tray insert of claim 8, wherein, The catalyst is placed on the upper tray to enable simultaneous catalytic reaction and separation during gas-liquid contact.

10. The tray insert of claim 1, wherein The upper tray channel is fixed to the upper tray by fasteners.

11. The tray insert of claim 1, wherein The gas phase nozzle is a multi-layered opening with an opening diameter of 5–20 mm.

12. The tray insert of claim 1, wherein The upper tray has several drain holes in the middle of the first opening, with a diameter of 2 to 10 mm, to ensure that the liquid phase in the upper tray is completely transferred to the lower tray during the liquid phase flow stage.

13. The tray insert of claim 1, wherein Multiple tower internals are arranged between the upper and lower tower trays, and are evenly spaced; the upper and lower tower trays form a set of tower trays, and multiple sets of tower trays are arranged inside the tower.

14. A gas-liquid mass transfer process characterized by, The tower internals described in any one of claims 1 to 13 are characterized by the following steps: A. Gas phase flow stage: Control the gas flow of the tray. The gas phase lifts the lower circular surface of the moving part, causing the moving part to move upward as a whole until the upper circular surface moves to the first flange. During this process, the gas phase moves from bottom to top and enters the space between the upper and lower trays through the second opening of the lower tray. Then, while lifting the upper circular surface, it draws in and carries the liquid phase from the upper tray into the channel of the upper tray, and sprays it out from the gas phase nozzle. At the same time, the gas-liquid mass and heat transfer is carried out while breaking the bubbles. B. Liquid phase flow stage: Control the tray to stop gas flow, and the moving parts move downward as a whole under the gravity of the liquid phase until the upper circular surface moves to the second flange and the lower circular surface moves to the third flange; during this process, the liquid phase flows from the upper tray through the gap at the bottom of the upper tray channel into the space between the upper and lower trays, and forms a liquid holding cavity on the lower tray. C. Next gas flow stage: Re-control the venting of the trays, and the gas phase lifts the lower circular surface of the moving part, causing the moving part to move upward as a whole; in the initial stage of upward movement, the second opening of the lower tray serves as a drain hole to release the liquid phase in the liquid holding chamber to the next set of trays, and step A is repeated.

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